Synthesis of AEI and Cu-AEI zeolites

ABSTRACT

A method of synthesizing a zeolite comprising the steps of: a. preparing an admixture containing (i) at least one source of alumina, (ii) at least one source of silica, and (iii) at least one structure directing agent (SDA) in hydroxide form, wherein the admixture is essentially free of alkali metals, wherein the at least one structure directing agent (SDA) in hydroxide form is N,N-diethyl-2,6-dimethylpiperidinium; and b. heating the admixture under autogenous pressure at a temperature and with stirring or mixing for a sufficient time to crystalize hydrogen-form zeolite crystals having an AEI framework.

CROSS REFERENCE TO RELATED APPLICATIONS

This application claims priority to U.S. Provisional Application No. 62/402,687, filed Sep. 30, 2016.

FIELD OF INVENTION

The present invention relates to the synthesis of hydrogen-form (H-form) zeolites having an AEI framework (H-AEI). The invention also relates to synthesis techniques for such zeolites and their use as a catalyst.

BACKGROUND

Zeolites are porous crystalline or quasi-crystalline aluminosilicates constructed of repeating SiO₄ and AlO₄ tetrahedral units. These units are linked together to form frameworks having regular intra-crystalline cavities and channels of molecular dimensions. Numerous types of synthetic zeolites have been synthesized and each has a unique framework based on the specific arrangement of its tetrahedral units. By convention, each framework type is assigned a unique three-letter code (e.g., “AEI”) by the International Zeolite Association (IZA).

Synthetic zeolites are typically produced using a structure directing agent (SDA), also referred to as a “template” or “templating agent”. SDAs are typically complex organic molecules that guide or direct the molecular shape and pattern of the zeolite's framework. Generally, the SDA serves to position hydrated silica and alumina and/or to serve as a mold around which the zeolite crystals form. After the crystals are formed, the SDA can be removed from the interior structure of the crystals, leaving a molecularly porous aluminosilicate cage.

Zeolites have numerous industrial applications including the catalytic treatment of exhaust gas from combustion of hydrocarbon fuels, such as internal combustion engines, gas turbines, coal-fired power plants, and the like. To improve catalytic performance, zeolites are frequently loaded with a transition metal, such as copper. In one example, a metal loaded zeolite can catalytically reduce the concentration of nitrogen oxides (NO_(x)) in the exhaust gas via a selective catalytic reduction (SCR) process.

AEI zeolite synthesis methods are known. These methods typically require a source of alkali metal ions, such as Na₂O. Before AEI zeolites can be used as an SCR catalyst, a significant portion of the alkali metal is desirably removed. It is difficult to completely remove all traces of alkali metal from the zeolite. Unfortunately, even residual amounts of sodium in an AEI zeolite can affect the amount of exchanged transition metal during catalyst preparation. In addition, at high temperatures (e.g., >800° C.), sodium can interact with the zeolite cage to form sodium-aluminates which, in turn, can collapse the cage structure, thereby reducing the high temperature durability of the zeolite. Accordingly, there is a need for an improved method for producing alkali-free AEI zeolites.

SUMMARY

Applicants have developed a unique series of hydrogen-form zeolites (H-zeolites) which are referred to herein as “JMZ-9 zeolite” or “JMZ-9”. This zeolite material contains the AEI framework structure as the primary phase and a template (SDA), and is essentially free of metal cations, such as sodium. In contrast to conventional zeolite synthesis, which uses alkali metal ions, it has been found that alkali-free AEI zeolites can be synthesized using a high concentration of one or more hydroxide-form SDAs and preferably using a reactive admixture that contains a high concentration of hydroxide-form SDAs relative to the concentrations of silica and/or alumina.

According to certain aspects of the invention, JMZ-9 is a novel composition comprising a synthetic H-form zeolite having an AEI framework structure as the primary crystalline phase, and an SDA, wherein the zeolite is essentially free of metal ions, including both alkali metal ions and transition metal ions.

These H-form AEI zeolites can undergo further processing to form a metal-loaded zeolite, such as copper-AEI, which can be used as a catalyst. Accordingly, in another aspect of the invention, provided is a catalyst composition comprising a synthetic zeolite having an AEI framework as the primary crystalline phase and a silica-to-alumina ratio of about 10 to about 50, wherein the zeolite has 0.1 to 7 weight percent exchanged transition metal and wherein the zeolite is essentially free of alkali metal. Preferred transition metals include copper and/or iron.

In another aspect of the invention, provided is a method for producing a H-form AEI zeolite comprising the steps of (a) preparing an admixture containing (i) at least one source of alumina, (ii) at least one source of silica, and (iii) at least one structure directing agent (SDA) in hydroxide form, wherein the admixture is essentially free of alkali metals, and optionally is also essentially free of other non-aluminum metal ions; and (b) heating the admixture under autogenous pressure at a temperature and with stirring or mixing for a sufficient time to crystalize H-form zeolite crystals having an AEI framework. The at least one SDA preferably includes about 20 to about 100 weight percent N,N-Diethyl-cis-2,6-dimethylpiperidium, based on the total weight percent of the SDAs. The SDA can contain from about 0 to about 80 weight percent N,N-Dimethyl-3,5-dimethylpiperidinium, with the balance being N,N-Diethyl-cis-2,6-dimethylpiperidium.

In another aspect of the invention, provided is a catalyst article for treating exhaust gas comprising a catalyst composition described herein, wherein the catalyst composition is disposed on and/or within a honeycomb monolith substrate.

And in yet another aspect of the invention, provided is a method for treating an exhaust gas comprising contacting a combustion exhaust gas containing NO_(x) and/or NH₃ with a catalyst article described herein to selectively reduce at least a portion of the NO_(x) into N₂ and H₂O and/or oxidize at least a portion of the NH₃.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows an XRD of calcined alkali-free AEI prepared in example 1.

FIG. 2A shows an SEM of alkali-free AEI (SAR≈30) prepared in example 1.

FIG. 2B shows an SEM of alkali-free AEI (SAR≈30) prepared in example 2.

FIG. 3 shows an SEM of alkali-free AEI (SAR≈30) prepared in example 3.

FIG. 4 shows an SEM of alkali-free AEI (SAR≈30) prepared in example 4.

FIG. 5A shows NOx conversions on 3% Cu.AEI (SAR≈20) and 2.5% Cu.H-AEI (SAR≈30).

FIG. 5B shows N₂O selectivity of reference 3% Cu.AEI (SAR≈20) and 2.5% Cu.H-AEI (SAR≈30).

FIG. 5C shows NOx conversions on 3% Cu.AEI (SAR≈20) and one-pot Cu-AEI (Example 5).

FIG. 5D shows N₂O selectivity of reference 3% Cu.AEI (SAR≈20) and one-pot Cu-AEI (Example 5).

FIG. 6 is a diagram showing an AEI-zeolite preparing according to one aspect of the invention as an SCR and/or ASC catalyst.

DETAILED DESCRIPTION

In general, JMZ-9 zeolites are aluminosilicates having an AEI framework structure in H-form as the primary crystalline phase and an SDA, and are essentially free of metal ions.

As used herein, the term “AEI” refers to an AEI crystalline structure as that code is recognized by the International Zeolite Association (IZA) Structure Commission. Aluminosilicates zeolites having an AEI framework as the primary crystalline phase means that the zeolite crystal comprises at least about 70 wt. %, at least about 80 wt. %, at least about 90 wt. %, at least about 95 wt. %, or at least about 99 wt. %, of AEI aluminosilicate framework, based on the total weight of aluminosilicate in the zeolite material. Preferably, any secondary crystalline phase comprises less than about 10 weight percent of the zeolite material, more preferably less than about 5 weight percent, and even more preferably less than about 2 weight percent.

As used herein, the term “essentially free of metal ions” means that alkali, alkaline-earth, and transition metal ions (other than aluminum) or sources thereof are not added as an intentional ingredient to the reaction admixture that is used to synthesize the zeolite crystals, and that if any alkali or alkaline earth metal ions are present in the zeolite, these metal ions are only present in an amount that is inconsequential to the intended catalytic activity of the zeolite.

JMZ-9 can contain less than about 0.1, preferably less than about 0.01, and more preferably less than about 0.001 weight percent of non-aluminum metal ions, based on the total weight of the zeolite.

JMZ-9 can contain less than about 0.1, preferably less than about 0.01, and more preferably less than about 0.001 weight percent of alkali metal ions, based on the total weight of the zeolite.

JMZ-9 can contain less than about 0.1, preferably less than about 0.01, and more preferably less than about 0.001 weight percent of sodium metal ions, based on the total weight of the zeolite.

JMZ-9 can contain less than about 0.1, preferably less than about 0.01, and more preferably less than about 0.001 weight percent of alkaline-earth metal ions, based on the total weight of the zeolite.

JMZ-9 can contain less than about 0.1, preferably less than about 0.01, and more preferably less than about 0.001 weight percent of transition metal ions, based on the total weight of the zeolite.

JMZ-9 can contain less than about 0.1, preferably less than about 0.01, and more preferably less than about 0.001 weight percent of copper metal ions, based on the total weight of the zeolite.

When used as a catalyst, JMZ-9 can include one or more post-synthesis, exchanged metals, typically in the form of metal ions and/or metal oxides. These post-synthesis exchanged metals are not part of the zeolite framework and are not present during zeolite synthesis (i.e., crystal formation). Exchanged metals include: (a) noble metals, such as gold and silver; (b) platinum group metals, including platinum, palladium, rhodium, and ruthenium; (c) transition metals, such as copper, iron, vanadium, manganese, and nickel; and (d) alkaline-earth metals, such as calcium. Transition metals are preferred, with copper and iron being preferred transition metals.

The method of metal exchange is not necessarily limited, but ion-exchange is a preferred method of loading metal onto the zeolite. Typically, a metal-exchanged JMZ-9 zeolite contains from about 0.1 to about 7 weight percent of an exchanged metal based on the total weight of the zeolite, particularly when the exchanged metal is copper or iron. Other metal loading ranges include from about 1 to about 6 weight percent, such as from about 2 to about 4 weight percent.

As used herein the terms “aluminosilicate zeolite” and “zeolite” are used interchangeably and mean a synthetic aluminosilicate molecular sieve having a framework constructed of alumina and silica (i.e., repeating SiO₄ and AlO₄ tetrahedral units), and preferably having a molar silica-to-alumina ratio (SAR) of at least about 20, for example about 22 to about 40.

The zeolites of the present invention are not silicoaluminophosphates (SAPOs) and thus do not have an appreciable amount of phosphorous in their framework. That is, the zeolite frameworks do not have phosphorous as a regular repeating unit and/or do not have an amount of phosphorous that would affect the basic physical and/or chemical properties of the material, particularly with respect to the material's capacity to selectively reduce NO_(x) over a broad temperature range. The amount of framework phosphorous can be less than 0.1 weight percent, preferably less than 0.01 or more preferably less than 0.001 weight percent, based on the total weight of the zeolite.

Zeolites, as used herein, are free or substantially free of framework metals, other than aluminum. Thus, a “zeolite” and a “metal-exchanged zeolite” are distinct from a “metal-substituted zeolite” (also referred to as “isomorphous substituted zeolite”), wherein the latter comprises a framework that contains one or more non-aluminum metals substituted into the zeolite's framework. Preferably, the JMZ-9 zeolite does not contain framework non-aluminum transition metals in an appreciable amount, e.g., less than about 10 ppm based on the total number of aluminum atoms in the crystal framework. Any post-synthesis metal loaded on the zeolite is preferably present as an ionic species within the interior channels and cavities of the zeolite framework.

In general, JMZ-9 zeolites are synthesized by preparing an admixture that is essentially free of alkali metals (including alkali metal ions) and that contains at least one source of alumina, at least one source of silica, and at least one structure directing agent (SDA) in hydroxide form. The admixture can also contain water. The admixture is preferably free from additional sources of hydroxide ions. The admixture is treated under conditions to crystalize H-form zeolite crystals having an AEI framework with a template within the framework.

The SDA in hydroxide form is preferably present in relatively large amounts compared to conventional synthesis techniques. For example, the silica (SiO₂) and SDA are preferably present in the admixture in a molar ratio of about 4:1 to about 1:1, preferably about 3:1 to about 1.5:1. Preferably, the molar ratio of silica-to-SDA and the molar ratio of silica-to-hydroxide is about the same, or at least within 10% of each other. It has been unexpectedly found that at these high concentrations, the SDA in hydroxide form functions both as the templating agent and the role of an alkaline source. Accordingly, no other alkali sources are needed. When alkali metal is eliminated from the admixture, the resulting AEI crystals are alkali-metal free.

The SDA(s) are selected for directing AEI synthesis. Examples of suitable SDAs include N,N-diethyl-cis-2,6-dimethylpiperidinium hydroxide (2,6-DMP) The anion associated with suitable SDA cations is hydroxide. Preferably, the reaction admixture and the resulting AEI zeolite are essentially free of non-hydroxide anions including halogen, e.g., fluoride, chloride, bromide and iodide, as well as acetate, sulfate, nitrate, tetrafluoroborate, and carboxylate.

In certain examples of the invention, the reaction admixture comprises 2,6-DMP as an SDA. The admixture can further comprise a second SDA. Preferably, the reaction admixture comprises at least about 20 weight percent 2,6-DMP, such as about 20 to about 100 percent, about 20 to about 50 percent, about 50 to about 100 percent, about 25 to about 75 percent, about 75 to about 100 percent, or about 40 to about 60 percent, based on the total weight of the SDAs. The remaining material to make up 100% of the weight of the SDA is a second SDA.

The reaction admixture can comprise a majority weight percent of 2,6-DMP based on the total weight the SDAs.

The abovementioned 2,6-DMP ranges can be used in combination with N,N-Dimethyl-3,5-dimethylpiperidinium (3,5-DMP), and preferably, 3,5-DMP comprises the balance of the SDAs.

The SDAs can comprise both 2,6-DMP and 3,5-DMP.

The SDAs can consist of (contain) only 2,6-DMP and 3,5-DMP.

At least about 20 weight percent 2,6-DMP can be used in combination with one or more intermediate hydrophobic templates (C/N⁺ ratio=8-12), such as 3,5-DMP, trimethyl cyclohexylammonium (TMCHA), tetraethylammonium (TEA), Dimethyldipropylammonium (DMDPA), tetrapropylammonium (TPA), tetraethylphosphonium (TEP).

Silica sources resulting in a high relative yield (greater than about 50%, greater than about 70%, greater than about 80%, or greater than about 90%) are preferred. Suitable silica sources include, without limitation, synthetic faujasites, fumed silica, silicates, precipitated silica, colloidal silica, silica gels, dealuminated zeolites, silicon alkoxides, and silicon hydroxides. Particularly preferred are synthetic faujasites such as zeolite Y. Preferred zeolite Y materials have a silica-to-alumina ratio (SAR) of about 10 to about 100, preferably about 12 to about 60.

Methods of the present invention unexpectedly have a relative yield on silica of greater than about 50%, greater than about 70%, greater than about 80%, or greater than about 90%. Inventors have found that the present synthesis methods result in a high relative yield on silica in an AEI zeolite synthesis process. As used herein, the term “relative yield” with respect to a chemical reactant, means the amount of the reactant (or derivative thereof) that is incorporated into a desired product as a fraction of the total amount of reactant introduced into the chemical process. Thus, the relative yield of a reactant can be calculated as follows: (Relative Yield) R=(R _(P))/(R _(T))

where R is the reactant, R_(P) is the total weight of reactant R (or derivative thereof) incorporated into the desired product, and R_(T) is total weight of reactant R introduced into the chemical process. Here, the relative yield serves to measure the effectiveness of the chemical process in utilizing the reactant. Here, “relative yield” is not synonymous with the term “overall relative yield” which means the relative yield for a chemical process as a whole, including for example, multiple sequential zeolite synthesis batch reactions. Thus, the overall relative yield on silica represents the total amount of silica that is incorporated into the total amount of zeolite produced across one or more sequential batches (vis-à-vis the amount of silica remaining in a discarded mother liquor) relative to the total amount of silica introduced into the process as a whole. The total amounts of these materials typically correspond to the material's total weight.

Typical alumina sources also are generally known and include synthetic faujasites, aluminates, alumina, other zeolites, aluminum colloids, boehmites, pseudo-boehmites, aluminum hydroxides, aluminum salts such as aluminum sulfate and alumina chloride, aluminum hydroxides and alkoxides, alumina gels. Particularly preferred are synthetic faujasites such as zeolite Y. Preferred zeolite Y materials have a silica-to-alumina ratio (SAR) of about 10 to about 100, preferably about 12 to about 60.

Preferably, the source of alumina and the source of silica are both synthetic faujasite (FAU). The synthetic faujasite may be single type of FAU zeolite or a mixture of two or more FAU zeolites.

The H-AEI synthesis is preferably conducted by combining predetermined relative amounts of the silica source, aluminum source, the SDA(s), and other components, such as water, under various mixing and heating regimens as will be readily apparent to those skilled in the art. Seed crystals, such as AEI zeolite, can also be included in the admixture. JMZ-9 can be prepared from a reaction mixture having the composition shown in Table 1 (shown as molar ratios). The reaction mixture can be in the form of a solution, gel, or paste. Silicon- and aluminum-containing reactants are expressed as SiO₂ and Al₂O₃, respectively.

TABLE 1 Ratios Typical Preferred SiO₂/OH 1-4 1.5-2.5 SiO₂/SDA(s) 1-4 1.5-2.5 H₂O/SiO₂ 10-40 15-30 alkali metal/SiO₂ 0 0 Al₂O₃/SiO₂ 0.02-0.05 0.025-0.04 

Reaction temperatures, mixing times and speeds, and other process parameters that are suitable for conventional AEI synthesis techniques are also generally suitable for the present invention. Without limitation, the following synthesis steps can be followed to synthesize JMZ-9. An aluminum source and a silica source (one or more zeolite Y materials, each with a SAR of about 10 to about 60) can be mixed in water and combined with an organic templating agent (e.g., 1,1-Diethyl-2,6-dimethylpiperidinium). The components can be mixed by stirring or agitation until a homogeneous mixture is formed. Hydrothermal crystallization can be conducted under autogenous pressure, at a temperature of about 100 to 200° C. for a duration of several days, such about 1-20 days, preferably about 1-3 days.

At the conclusion the crystallization period, the resulting solids are separated from the remaining reaction liquid by standard mechanical separation techniques, such as vacuum filtration. The recovered solids are then rinsed with deionized water, and dried at an elevated temperature (e.g., 75-150° C.) for several hours (e.g., about 4 to 24 hours). The drying step can be performed under vacuum or at atmospheric pressure.

The dried JMZ-9 crystals are preferably calcined, but can also be used without calcination.

It will be appreciated that the foregoing sequence of steps, as well as each of the above-mentioned periods of time and temperature values, are merely exemplary and can be varied.

The JMZ-9 zeolite can be useful as a catalyst in certain applications, preferably with a post-synthesis metal exchange wherein one or more catalytic metals is exchanged into the channels and/or cavities of the zeolite. Examples of metals that can be post-zeolite synthesis exchanged or impregnated include (a) transition metals, including copper, nickel, zinc, iron, tungsten, molybdenum, cobalt, titanium, zirconium, manganese, chromium, vanadium, niobium, tin, bismuth, and antimony; (b) noble metals including platinum group metals (PGMs), such as ruthenium, rhodium, palladium, indium, platinum, and precious metals such as gold and silver, (c) alkaline earth metals such as beryllium, magnesium, calcium, strontium, and barium; and (d) rare earth metals such as lanthanum, cerium, praseodymium, neodymium, europium, terbium, erbium, ytterbium, and yttrium. Preferred transition metals for post-synthesis exchange are base metals, and preferred base metals are those selected from the group consisting of copper, iron, manganese, vanadium, nickel, and mixtures thereof. Metals incorporated post-synthesis can be added to the molecular sieve via any known technique such as ion exchange, impregnation, isomorphous substitution, etc. The amount of metal post-synthesis exchanged can be from about 0.1 to about 7 weight percent, for example about 2 to about 5 weight percent, based on the total weight of the zeolite.

The metal-containing zeolite preferably contains post-synthesis exchanged alkaline earth metal, particularly calcium and/or magnesium, disposed within the channels and/or cavities of the zeolite framework. Thus, the metal-containing zeolite of the present invention can have transition metals (T_(M)), such as copper or iron, incorporated into the zeolite channels and/or cavities during synthesis and have one or more exchanged alkaline earth metals (A_(M)), such as calcium or potassium, incorporated post-synthesis. The alkaline earth metal can be present in an amount relative to the transition metal that is present. For example, T_(M) and A_(M) are preferably present, respectively, in a molar ratio of about 15:1 to about 1:1, about 10:1 to about 2:1, about 10:1 to about 3:1, or about 6:1 to about 4:1, particularly were T_(M) is copper and A_(M) is calcium. Preferably, the relative cumulative amount of transition metal (T_(M)) and alkaline earth metal (A_(M)) is present in the zeolite material in an amount relative to the amount of aluminum in the zeolite, namely the framework aluminum. As used herein, the (T_(M)+A_(M)):Al ratio is based on the relative molar amounts of T_(M)+A_(M) to molar framework Al in the corresponding zeolite. Preferably, the catalyst material has a (T_(M)+A_(M)):Al ratio of not more than about 0.6 or about 0.5 and can be from about 0.05 to about 0.5, about 0.1 to about 0.4, or about 0.1 to about 0.2.

Preferably, Ce is impregnated post-synthesis into the JMZ-9, for example, by adding Ce nitrate to a copper promoted zeolite via a conventional incipient wetness technique. Preferably, the cerium in the catalyst material is present in a concentration of at least about 1 weight percent, based on the total weight of the zeolite. Preferred concentrations include at least about 2.5 weight percent, at least about 5 weight percent, at least about 8 weight percent, at least about 10 weight percent, about 1.35 to about 13.5 weight percent, about 2.7 to about 13.5 weight percent, about 2.7 to about 8.1 weight percent, about 2 to about 4 weight percent, about 2 to about 9.5 weight percent, and about 5 to about 9.5 weight percent, based on the total weight of the zeolite.

Preferably, the cerium concentration in the catalyst material can be about 50 to about 550 g/ft³, from about 75 to about 350 g/ft³, from about 100 to about 300 g/ft³, or from about 100 to about 250 g/ft³. Ce can be present at concentrations above 100 g/ft³, above 200 g/ft³, above 300 g/ft³, above 400 g/ft³, or above 500 g/ft³.

The catalyst can be part of a washcoat composition, the washcoat can further comprise a binder containing Ce or ceria. Preferably, the Ce containing particles in the binder are significantly larger than the Ce containing particles in the catalyst.

Applicants further discovered that the foregoing synthesis procedure permits adjusting the SAR of the catalyst based on the composition of the starting synthesis mixture. SARs of 10-50, 20-40, 30-40, 10-15, and 25-35, for example, can be selectively achieved based on the composition of the starting synthesis mixture and/or adjusting other process variables. The SAR of zeolites can be determined by conventional analysis. This ratio is meant to represent, as closely as possible, the ratio in the rigid atomic framework of the zeolite crystal and to exclude silicon or aluminum in the binder or, in cationic or other form, within the channels. It will be appreciated that it can be extremely difficult to directly measure the SAR of zeolite after it has been combined with a binder material. Accordingly, the SAR has been expressed hereinabove in term of the SAR of the parent zeolite, i.e., the zeolite used to prepare the catalyst, as measured prior to the combination of this zeolite with the other catalyst components.

The foregoing synthesis procedure can result in zeolite crystals of uniform size and shape with relatively low amounts of agglomeration. In addition, the synthesis procedure can result in zeolite crystals having a mean crystalline size of about 0.2 to about 10 μm, about 0.5 to about 5 μm, about 0.2 to about 1 μm, about 1 to about 5 μm, about 3 to about 7 μm, and the like. Preferably, large crystals are milled using a jet mill or other particle-on-particle milling technique to an average size of about 1.0 to about 1.5 micron to facilitate washcoating a slurry containing the catalyst to a substrate, such as a flow-through monolith. Alternatively, the crystals can be unmilled.

Crystal size is the length of one edge of a face of the crystal. The crystal size is based on individual crystals (including twinned crystals) but does not include agglomerations of crystals. Direct measurement of the crystal size can be performed using microscopy methods, such as SEM and TEM. Other techniques for determining mean particle size, such as laser diffraction and scattering can also be used.

In addition to the mean crystal size, catalyst compositions preferably have a majority of the crystal sizes are greater than about 0.2 μm, preferably between about 0.5 and about 5 μm, about 0.7 to about 5 μm, about 1 to about 5 μm, about 1.5 to about 5.0 μm, about 1.5 to about 4.0 μm, about 2 to about 5 μm, or about 1 μm to about 10 μm.

Catalysts of the present invention are particularly applicable for heterogeneous catalytic reaction systems (i.e., solid catalyst in contact with a gas reactant). To improve contact surface area, mechanical stability, and/or fluid flow characteristics, the catalysts can be disposed on and/or within a substrate, preferably a porous substrate. Preferably, a washcoat containing the catalyst can be applied to an inert substrate, such as corrugated metal plate or a honeycomb cordierite brick. Alternatively, the catalyst can be kneaded along with other components such as fillers, binders, and reinforcing agents, into an extrudable paste which is then extruded through a die to form a honeycomb brick. Accordingly, in a catalyst article comprising a JMZ-9 catalyst described herein can be coated on and/or incorporated into a substrate.

Certain aspects of the invention provide a catalytic washcoat. The washcoat comprising the JMZ-9 catalyst described herein is preferably a solution, suspension, or slurry. Suitable coatings include surface coatings, coatings that penetrate a portion of the substrate, coatings that permeate the substrate, or some combination thereof.

A washcoat can also include non-catalytic components, such as fillers, binders, stabilizers, rheology modifiers, and other additives, including one or more of alumina, silica, non-zeolite silica alumina, titania, zirconia, ceria. The catalyst composition may comprise pore-forming agents such as graphite, cellulose, starch, polyacrylate, and polyethylene, and the like. These additional components do not necessarily catalyze the desired reaction, but instead improve the catalytic material's effectiveness, for example, by increasing its operating temperature range, increasing contact surface area of the catalyst, increasing adherence of the catalyst to a substrate, etc. Preferably, the washcoat loading is >0.3 g/in³, >1.2 g/in³, >1.5 g/in³, >1.7 g/in³ or >2.00 g/in³, and preferably <3.5 g/in³, or <2.5 g/in³. The washcoat can be applied to a substrate at a loading of about 0.8 to 1.0 g/in³, 1.0 to 1.5 g/in³, or 1.5 to 2.5 g/in³.

Two of the most common substrate designs are plate and honeycomb. Preferred substrates, particularly for mobile applications, include flow-through monoliths having a so-called honeycomb geometry that comprise multiple adjacent, parallel channels that are open on both ends and generally extend from the inlet face to the outlet face of the substrate and result in a high-surface area-to-volume ratio. For certain applications, the honeycomb flow-through monolith preferably has a high cell density, for example about 600 to 800 cells per square inch, and/or an average internal wall thickness of about 0.18-0.35 mm, preferably about 0.20-0.25 mm. For certain other applications, the honeycomb flow-through monolith preferably has a low cell density of about 150-600 cells per square inch, more preferably about 200-400 cells per square inch. Preferably, the honeycomb monoliths are porous. In addition to cordierite, silicon carbide, silicon nitride, ceramic, and metal, other materials that can be used for the substrate include aluminum nitride, silicon nitride, aluminum titanate, α-alumina, mullite, e.g., acicular mullite, pollucite, a thermet such as Al₂OsZFe, Al₂O₃/Ni or B₄CZFe, or composites comprising segments of any two or more thereof. Preferred materials include cordierite, silicon carbide, and alumina titanate.

Plate-type catalysts have lower pressure drops and are less susceptible to plugging and fouling than the honeycomb types, which is advantageous in high efficiency stationary applications, but plate configurations can be much larger and more expensive. A honeycomb configuration is typically smaller than a plate type, which is an advantage in mobile applications, but has higher pressure drops and plug more easily. Preferably, the plate substrate is constructed of metal, preferably corrugated metal.

The invention is a catalyst article can be made by a process described herein. Preferably, the catalyst article is produced by a process that includes the steps of applying a JMZ-9 catalyst composition, preferably as a washcoat, to a substrate as a layer either before or after at least one additional layer of another composition for treating exhaust gas has been applied to the substrate. The one or more catalyst layers on the substrate, including the JMZ-9 catalyst layer, are arranged in consecutive layers. As used herein, the term “consecutive” with respect to catalyst layers on a substrate means that each layer is contact with its adjacent layer(s) and that the catalyst layers as a whole are arranged one on top of another on the substrate.

The JMZ-9 catalyst can be disposed on the substrate as a first layer and another composition, such as an oxidation catalyst, reduction catalyst, scavenging component, or NO_(x) storage component, can be disposed on the substrate as a second layer. Alternatively, the JMZ-9 catalyst can be disposed on the substrate as a second layer and another composition, such as such as an oxidation catalyst, reduction catalyst, scavenging component, or NO_(x) storage component, is disposed on the substrate as a first layer. As used herein the terms “first layer” and “second layer” are used to describe the relative positions of catalyst layers in the catalyst article with respect to the normal direction of exhaust gas flow-through, past, and/or over the catalyst article. Under normal exhaust gas flow conditions, exhaust gas contacts the first layer prior to contacting the second layer. The second layer can be applied to an inert substrate as a bottom layer and the first layer is top layer that is applied over the second layer as a consecutive series of sub-layers. The exhaust gas can penetrate (and hence contacts) the first layer, before contacting the second layer, and subsequently returns through the first layer to exit the catalyst component. The first layer can be a first zone disposed on an upstream portion of the substrate and the second layer is disposed on the substrate as a second zone, wherein the second zone is downstream of the first.

The catalyst article can be produced by a process that includes the steps of applying a JMZ-9 catalyst composition, preferably as a washcoat, to a substrate as a first zone, and subsequently applying at least one additional composition for treating an exhaust gas to the substrate as a second zone, wherein at least a portion of the first zone is downstream of the second zone. Alternatively, the JMZ-9 catalyst composition can be applied to the substrate in a second zone that is downstream of a first zone containing the additional composition. Examples of additional compositions include oxidation catalysts, reduction catalysts, scavenging components (e.g., for sulfur, water, etc.), or NO_(x) storage components.

To reduce the amount of space required for an exhaust system, individual exhaust components can be designed to perform more than one function. For example, applying an SCR catalyst to a wall-flow filter substrate instead of a flow-through substrate serves to reduce the overall size of an exhaust treatment system by allowing one substrate to serve two functions, namely catalytically reducing NO_(x) concentration in the exhaust gas and mechanically removing soot from the exhaust gas. Accordingly, the substrate can be a honeycomb wall-flow filter or partial filter. Wall-flow filters are similar to flow-through honeycomb substrates in that they contain a plurality of adjacent, parallel channels. However, the channels of flow-through honeycomb substrates are open at both ends, whereas the channels of wall-flow substrates have one end capped, wherein the capping occurs on opposite ends of adjacent channels in an alternating pattern. Capping alternating ends of channels prevents the gas entering the inlet face of the substrate from flowing straight through the channel and existing. Instead, the exhaust gas enters the front of the substrate and travels into about half of the channels where it is forced through the channel walls prior to entering the second half of the channels and exiting the back face of the substrate.

The substrate wall has a porosity and pore size that is gas permeable, but traps a major portion of the particulate matter, such as soot, from the gas as the gas passes through the wall. Preferred wall-flow substrates are high efficiency filters. Wall flow filters for use with the present invention preferably have an efficiency of least 70%, at least about 75%, at least about 80%, or at least about 90%. The efficiency can be in a range from about 75 to about 99%, about 75 to about 90%, about 80 to about 90%, or about 85 to about 95%. Here, efficiency is relative to soot and other similarly sized particles and to particulate concentrations typically found in conventional diesel exhaust gas. For example, particulates in diesel exhaust can range in size from 0.05 microns to 2.5 microns. Thus, the efficiency can be based on this range or a sub-range, such as 0.1 to 0.25 microns, 0.25 to 1.25 microns, or 1.25 to 2.5 microns.

Porosity is a measure of the percentage of void space in a porous substrate and is related to backpressure in an exhaust system: generally, the lower the porosity, the higher the backpressure. Preferably, the porous substrate has a porosity of about 30 to about 80%, for example about 40 to about 75%, about 40 to about 65%, or from about 50 to about 60%.

The pore interconnectivity, measured as a percentage of the substrate's total void volume, is the degree to which pores, void, and/or channels, are joined to form continuous paths through a porous substrate, i.e., from the inlet face to the outlet face. In contrast to pore interconnectivity is the sum of closed pore volume and the volume of pores that have a conduit to only one of the surfaces of the substrate. Preferably, the porous substrate has a pore interconnectivity volume of at least about 30%, more preferably at least about 40%.

The mean pore size of the porous substrate is also important for filtration. Mean pore size can be determined by any acceptable means, including by mercury porosimetry. The mean pore size of the porous substrate should be of a high enough value to promote low backpressure, while providing an adequate efficiency by either the substrate per se, by promotion of a soot cake layer on the surface of the substrate, or combination of both. Preferred porous substrates have a mean pore size of about 10 to about 40 μm, for example about 20 to about 30 μm, about 10 to about 25 μm, about 10 to about 20 μm, about 20 to about 25 μm, about 10 to about 15 μm, and about 15 to about 20 μm.

In general, the production of an extruded solid body containing the JMZ-9 catalyst involves blending the JMZ-9 catalyst, a binder, an optional organic viscosity-enhancing compound into a homogeneous paste which is then added to a binder/matrix component or a precursor thereof and optionally one or more of stabilized ceria, and inorganic fibers. The blend is compacted in a mixing or kneading apparatus or an extruder. The mixtures have organic additives such as binders, pore formers, plasticizers, surfactants, lubricants, dispersants as processing aids to enhance wetting and therefore produce a uniform batch. The resulting plastic material is then molded, in particular using an extrusion press or an extruder including an extrusion die, and the resulting moldings are dried and calcined. The organic additives are “burnt out” during calcinations of the extruded solid body. A JMZ-9 catalyst can also be washcoated or otherwise applied to the extruded solid body as one or more sub-layers that reside on the surface or penetrate wholly or partly into the extruded solid body.

Extruded solid bodies containing JMZ-9 catalysts according to the present invention generally comprise a unitary structure in the form of a honeycomb having uniform-sized and parallel channels extending from a first end to a second end thereof. Channel walls defining the channels are porous. Typically, an external “skin” surrounds a plurality of the channels of the extruded solid body. The extruded solid body can be formed from any desired cross section, such as circular, square or oval. Individual channels in the plurality of channels can be square, triangular, hexagonal, circular etc. Channels at a first, upstream end can be blocked, e.g. with a suitable ceramic cement, and channels not blocked at the first, upstream end can also be blocked at a second, downstream end to form a wall-flow filter. Typically, the arrangement of the blocked channels at the first, upstream end resembles a checker-board with a similar arrangement of blocked and open downstream channel ends.

The binder/matrix component is preferably selected from the group consisting of cordierite, nitrides, carbides, borides, intermetallics, lithium aluminosilicate, a spinel, an optionally doped alumina, a silica source, titania, zirconia, titania-zirconia, zircon and mixtures of any two or more thereof. The paste can optionally contain reinforcing inorganic fibers selected from the group consisting of carbon fibers, glass fibers, metal fibers, boron fibers, alumina fibers, silica fibers, silica-alumina fibers, silicon carbide fibers, potassium titanate fibers, aluminum borate fibers and ceramic fibers.

The alumina binder/matrix component is preferably gamma alumina, but can be any other transition alumina, i.e., alpha alumina, beta alumina, chi alumina, eta alumina, rho alumina, kappa alumina, theta alumina, delta alumina, lanthanum beta alumina and mixtures of any two or more such transition aluminas. It is preferred that the alumina is doped with at least one non-aluminum element to increase the thermal stability of the alumina. Suitable alumina dopants include silicon, zirconium, barium, lanthanides and mixtures of any two or more thereof. Suitable lanthanide dopants include La, Ce, Nd, Pr, Gd and mixtures of any two or more thereof.

Sources of silica can include a silica sol, quartz, fused or amorphous silica, sodium silicate, an amorphous aluminosilicate, an alkoxysilane, a silicone resin binder such as methylphenyl silicone resin, a clay, talc or a mixture of any two or more thereof. Of this list, the silica can be SiO₂ as such, feldspar, mullite, silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-berylia, silica-titania, ternary silica-alumina-zirconia, ternary silica-alumina-magnesia, temary-silica-magnesia-zirconia, temary silica-alumina-thoria and mixtures of any two or more thereof.

Preferably, the JMZ-9 catalyst is dispersed throughout, and preferably evenly throughout, the entire extruded catalyst body.

Where any of the above extruded solid bodies are made into a wall-flow filter, the porosity of the wall-flow filter can be from 30-80%, such as from 40-70%. Porosity and pore volume and pore radius can be measured e.g. using mercury intrusion porosimetry.

The JMZ-9 catalyst described herein can promote the reaction of a reductant, preferably ammonia, with nitrogen oxides to selectively form elemental nitrogen (N₂) and water (H₂O). Thus, the catalyst can be formulated to favor the reduction of nitrogen oxides with a reductant (i.e., an SCR catalyst). Examples of such reductants include hydrocarbons (e.g., C3-C6 hydrocarbons) and nitrogenous reductants such as ammonia and ammonia hydrazine or any suitable ammonia precursor, such as urea ((NH₂)₂CO), ammonium carbonate, ammonium carbamate, ammonium hydrogen carbonate or ammonium formate.

The JMZ-9 catalyst described herein can also promote the oxidation of ammonia. Thus, the catalyst can be formulated to favor the oxidation of ammonia with oxygen, particularly a concentrations of ammonia typically encountered downstream of an SCR catalyst (e.g., ammonia oxidation (AMOX) catalyst, such as an ammonia slip catalyst (ASC)). The JMZ-9 catalyst can be disposed as a top layer over an oxidative under-layer, wherein the under-layer comprises a platinum group metal (PGM) catalyst or a non-PGM catalyst. Preferably, the catalyst component in the underlayer is disposed on a high surface area support, including but not limited to alumina.

An SCR and AMOX operations can be performed in series, wherein both processes utilize a catalyst comprising the JMZ-9 catalyst described herein, and wherein the SCR process occurs upstream of the AMOX process. For example, an SCR formulation of the catalyst can be disposed on the inlet side of a filter and an AMOX formulation of the catalyst can be disposed on the outlet side of the filter.

Accordingly, provided is a method for the reduction of NO_(x) compounds or oxidation of NH₃ in a gas, which comprises contacting the gas with a catalyst composition described herein for the catalytic reduction of NO_(x) compounds for a time sufficient to reduce the level of NO_(x) compounds and/or NH₃ in the gas. Also provided is a catalyst article having an ammonia slip catalyst disposed downstream of a selective catalytic reduction (SCR) catalyst. The ammonia slip catalyst can oxidize at least a portion of any nitrogenous reductant that is not consumed by the selective catalytic reduction process. For example, the ammonia slip catalyst can be disposed on the outlet side of a wall flow filter and an SCR catalyst is disposed on the upstream side of a filter. The ammonia slip catalyst can be disposed on the downstream end of a flow-through substrate and an SCR catalyst is disposed on the upstream end of the flow-through substrate. The ammonia slip catalyst and SCR catalyst can be disposed on separate bricks within the exhaust system. These separate bricks can be adjacent to, and in contact with, each other or separated by a specific distance, provided that they are in fluid communication with each other and provided that the SCR catalyst brick is disposed upstream of the ammonia slip catalyst brick.

The SCR and/or AMOX process can be performed at a temperature of at least 100° C. The process(es) can occur at a temperature from about 150° C. to about 750° C. Preferably the temperature range is from about 175 to about 550° C. or from about 175 to about 400° C. Alternatively, the temperature range is about 450 to about 900° C., preferably about 500 to about 750° C., about 500 to about 650° C., about 450 to about 550° C., or about 650 to about 850° C. Temperatures greater than about 450° C. are particularly useful for treating exhaust gases from a heavy or light duty diesel engine that is equipped with an exhaust system comprising (optionally catalyzed) diesel particulate filters which are regenerated actively, e.g. by injecting hydrocarbon into the exhaust system upstream of the filter, wherein the zeolite catalyst for use in the present invention is located downstream of the filter.

According to another aspect of the invention, provided is a method for the reduction of NO_(X) compounds and/or oxidation of NH₃ in an exhaust gas, which comprises contacting the exhaust gas with a catalyst described herein in the presence of a reducing agent for a time sufficient to reduce the level of NO_(X) compounds in the gas. These methods can further comprise one or more of the following steps: (a) accumulating and/or combusting soot that is in contact with the inlet of a catalytic filter; (b) introducing a nitrogenous reducing agent into the exhaust gas stream prior to contacting the catalyst in an SCR filter, preferably with no intervening catalytic steps involving the treatment of NO_(x) and the reductant; (c) generating NH₃ over a NO_(x) adsorber catalyst or lean NO_(x) trap, and preferably using such NH₃ as a reductant in a downstream SCR reaction; (d) contacting the exhaust gas stream with a DOC to oxidize hydrocarbon based soluble organic fraction (SOF) and/or carbon monoxide into CO₂, and/or oxidize NO into NO₂, which, in turn, can be used to oxidize particulate matter in particulate filter; and/or reduce the particulate matter (PM) in the exhaust gas; and (e) contacting the exhaust gas with an ammonia slip catalyst, preferably downstream of the SCR catalyst to oxidize most, if not all, of the ammonia prior to emitting the exhaust gas into the atmosphere or passing the exhaust gas through a recirculation loop prior to exhaust gas entering/re-entering the engine.

All or at least a portion of the nitrogen-based reductant, particularly NH₃, for consumption in the SCR process can be supplied by a NO_(X) adsorber catalyst (NAC), a lean NO_(X) trap (LNT), or a NO_(X) storage/reduction catalyst (NSRC), disposed upstream of the SCR catalyst, e.g., a SCR catalyst of the present invention disposed on a wall-flow filter. NAC components useful in the present invention include a catalyst combination of a basic material (such as alkali metal, alkaline earth metal or a rare earth metal, including oxides of alkali metals, oxides of alkaline earth metals, and combinations thereof), and a precious metal (such as platinum), and optionally a reduction catalyst component, such as rhodium. Specific types of basic material useful in the NAC include cesium oxide, potassium oxide, magnesium oxide, sodium oxide, calcium oxide, strontium oxide, barium oxide, and combinations thereof. The precious metal is preferably present at about 10 to about 200 g/ft³, such as 20 to 60 g/ft³. Alternatively, the precious metal of the catalyst can have an average concentration from about 40 to about 100 grams/ft³.

Under certain conditions, during the periodically rich regeneration events, NH₃ can be generated over a NO_(x) adsorber catalyst. The SCR catalyst downstream of the NO_(x) adsorber catalyst can improve the overall system NO_(x) reduction efficiency. In the combined system, the SCR catalyst is capable of storing the released NH₃ from the NAC catalyst during rich regeneration events and utilizes the stored NH₃ to selectively reduce some or all of the NO_(x) that slips through the NAC catalyst during the normal lean operation conditions.

The method for treating exhaust gas as described herein can be performed on an exhaust gas derived from a combustion process, such as from an internal combustion engine (whether mobile or stationary), a gas turbine and coal or oil fired power plants. These methods may also be used to treat gas from industrial processes such as refining, from refinery heaters and boilers, furnaces, the chemical processing industry, coke ovens, municipal waste plants and incinerators, etc. The method can be used for treating exhaust gas from a vehicular lean burn internal combustion engine, such as a diesel engine, a lean-burn gasoline engine or an engine powered by liquid petroleum gas or natural gas.

In certain aspects, the invention is a system for treating exhaust gas generated by combustion process, such as from an internal combustion engine (whether mobile or stationary), a gas turbine, coal or oil fired power plants, and the like. Such systems include a catalytic article comprising the JMZ-9 catalyst described herein and at least one additional component for treating the exhaust gas, wherein the catalytic article and at least one additional component are designed to function as a coherent unit.

The system can comprise a catalytic article comprising a JMZ-9 catalyst described herein, a conduit for directing a flowing exhaust gas, a source of nitrogenous reductant disposed upstream of the catalytic article. The system can include a controller for the metering the nitrogenous reductant into the flowing exhaust gas only when it is determined that the zeolite catalyst is capable of catalyzing NO_(x) reduction at or above a desired efficiency, such as at above 100° C., above 150° C. or above 175° C. The metering of the nitrogenous reductant can be arranged such that 60% to 200% of theoretical ammonia is present in exhaust gas entering the SCR catalyst calculated at 1:1 NH₃/NO and 4:3 NH₃/NO₂.

The system can comprise an oxidation catalyst (e.g., a diesel oxidation catalyst (DOC)) for oxidizing nitrogen monoxide in the exhaust gas to nitrogen dioxide can be located upstream of a point of metering the nitrogenous reductant into the exhaust gas. The oxidation catalyst can be adapted to yield a gas stream entering the SCR zeolite catalyst having a ratio of NO to NO₂ of from about 4:1 to about 1:3 by volume, e.g. at an exhaust gas temperature at oxidation catalyst inlet of 250° C. to 450° C. The oxidation catalyst can comprise at least one platinum group metal, such as platinum, palladium, or rhodium, or combinations thereof, coated on a flow-through monolith substrate. The at least one platinum group metal can be platinum, palladium or a combination of both platinum and palladium. The platinum group metal can be supported on a high surface area washcoat component such as alumina, a zeolite such as an aluminosilicate zeolite, silica, non-zeolite silica alumina, ceria, zirconia, titania or a mixed or composite oxide containing both ceria and zirconia.

A suitable filter substrate can be located between the oxidation catalyst and the SCR catalyst. Filter substrates can be selected from any of those mentioned above, e.g. wall flow filters. Where the filter is catalyzed, e.g. with an oxidation catalyst of the kind discussed above, preferably the point of metering nitrogenous reductant is located between the filter and the zeolite catalyst. Alternatively, if the filter is un-catalyzed, the means for metering nitrogenous reductant can be located between the oxidation catalyst and the filter.

The metal-promoted small pore JMZ-9 zeolite catalyst described herein can also be a passive NOx absorber (PNA) catalyst (i.e. it has PNA activity). Such catalyst can be prepared according to the method described in WO 2012/166868 (also published as U.S. 2012308439) (both of which are hereby incorporated by reference.), and the promoter metal can comprise a noble metal.

When the noble metal comprises, or consists of, palladium (Pd) and a second metal, then the ratio by mass of palladium (Pd) to the second metal is >1:1. More preferably, the ratio by mass of palladium (Pd) to the second metal is >1:1 and the molar ratio of palladium (Pd) to the second metal is >1:1. The aforementioned ratio of palladium relates to the amount of palladium present as part of the PNA catalyst. It does not include any palladium that may be present on the support material. The PNA catalyst may further comprise a base metal. Thus, the PNA catalyst may comprise, or consist essentially of, a noble metal, a small pore zeolite as described herein and optionally a base metal.

The base metal can be selected from the group consisting of iron (Fe), copper (Cu), manganese (Mn), chromium (Cr), cobalt (Co), nickel (Ni), zinc (Zn) and tin (Sn), as well as mixtures of two or more thereof. It is preferred that the base metal is selected from the group consisting of iron, copper and cobalt, more preferably iron and copper. Even more preferably, the base metal is iron.

Alternatively, the PNA catalyst can be substantially free of a base metal, such as a base metal selected from the group consisting of iron (Fe), copper (Cu), manganese (Mn), chromium (Cr), cobalt (Co), nickel (Ni), zinc (Zn) and tin (Sn), as well as mixtures of two or more thereof. Thus, the PNA catalyst may not comprise a base metal.

In general, it is preferred that the PNA catalyst does not comprise a base metal.

It can be preferable that the PNA catalyst is substantially free of barium (Ba), more preferably the PNA catalyst is substantially free of an alkaline earth metal. Thus, the PNA catalyst may not comprise barium, preferably the PNA catalyst does not comprise an alkaline earth metal.

Turning to FIG. 6, shown is an SCR and/or ASC catalyst 10, an exhaust gas 20, a purified gas 22, and a direction of flow through the SCR and/or ASC catalyst 30. The exhaust gas 20 has an inlet concentration of NO and/or NO₂ and the purified gas 22 has an outlet concentration of NO and/or NO₂ that is less than the inlet concentration. The purified gas 22 also has an outlet concentration of N₂O that is less than the inlet concentration of NO and/or NO₂.

Although the description above contains many specifics, these are merely provided to illustrate the invention and should not be constructed as limitations of the invention's scope. It should be also noted that many specifics could be combined in various ways in a single or multiple embodiments. Thus it will be apparent to those skilled in the art that various modifications and variations can be made in the processes, catalysts, and methods of the present invention without departing from the spirit or scope of the invention.

EXAMPLES

Materials produced in the examples described below were characterized by one or more of the following analytic methods. Powder X-ray diffraction (PXRD) patterns were collected Bruker D8 powder diffractometer using a CuKα radiation (40 kV, 40 mA) at a step size of 0.02° and a 1 s per step between 5° and 50° (2θ). Scanning electron microscopy (SEM) images and chemical compositions by energy-dispersive X-ray spectroscopy (EDX) were obtained on an Auriga 60 CrossBeam (FIB/FE-SEM) microscope, operating at an acceleration voltage of 1.5-3 keV, and a current of 10 μA. The micropore volume and surface area were measured using N₂ at 77 K on a Micrometrics 3Flex surface characterization analyzer.

Reagents:

Zeolite Y [CBV712 (SAR˜12), CBV720 (SAR˜30-32) from Zeolyst], DI water, N,N-diethyl-cis 2,6-dimethylpiperidium hydroxide (2,6-DMP-OH, 22% wt), N,N-dimethyl-3,5-dimethylpiperidium (34% wt), tetrapropylammonium (TPA, 40% wt), Triethylenetetramine (TETA, Sigma), CuSO₄.5H₂O (Sigma).

Example 1: Preparation of H-AEI Zeolite Using 2,6-DMP as the SDA

13.69 g of 2,6-DMP-OH was mixed with 3.1 g of water. Then, the solution was stirred for about 5 minutes. Finally, 2.16 g of zeolite Y (CBV 720) as both aluminum and silica sources were added under stirring for another 5 minutes. The final gel mixture having molar compositions of 25 H₂O:1 SiO₂:0.033 Al₂O₃:0.5 2,6-DMP-OH was heated and rotated (45 rpm for 23 ml reactor) at 155° C. for 5 days.

To obtain the AEI powder product, the autoclaves were cooled to room temperature in air and the crystalline product was recovered by filtration, washed several times with deionized water and dried at 80° C. overnight in a drying oven. The as-made product (JMZ-9) was calcined at 580° C./8 hours in air with ramping rate of 3° C./min. Samples of the dried product were analysed by XRD and SEM as described above. Analysis of the calcined product by powder XRD (FIG. 1) indicated that the product had an AEI structure. An SEM (FIG. 2a ) of the calcined product showed that the material has cuboid morphology with crystal size of about 0.2 to about 0.5 micron. N₂ adsorption measurements of the calcined product showed that the product had a BET surfaces area of ˜680 m²/g, a pore volume of ˜0.27 cm³/g, and had a cubic morphology. The calcined product had an SAR of about 30.

Example 2: Preparation of H-AEI Zeolite Using 2,6-DMP as the SDA and a Mixture of Faujasite Zeolites as Both Si and Al Sources

13.69 g of 2,6-DMP-OH was mixed with 3.1 g of water. Then, the solution was stirred for about 5 minutes. Finally, a mixture of 0.45 g zeolite Y (CBV712) and 1.72 g of zeolite Y (CBV 720) as both aluminum and silica sources was added under stirring for another 5 minutes. The reaction was heated and rotated (45 rpm for 23 ml reactor) at 155° C. for 5 days. To obtain the AEI powder product, the autoclaves were cooled to room temperature in air and the crystalline product was recovered by filtration, washed several times with deionized water and dried at 80° C. overnight in a drying oven. The as-made product (JMZ-9) was calcined at 580° C./8 hours in air with ramping rate of 3° C./min. Samples of the dried product were analysed by XRD and SEM as described above. Analysis of the as made product by powder XRD indicated that the product had an AEI structure. An SEM of the calcined product showed that the material has cuboid morphology with crystal size of about 0.2 to about 0.5 micron (FIG. 2b ). The calcined product had an SAR of about 24. N₂ adsorption measurements of the calcined product showed that the product had a pore volume of ˜0.28 cm³/g.

Example 3: Preparation of H-AEI Zeolite Using a Mixture of 2,6-DMP-OH and 3,5-DMP-OH as the SDAs

H-AEI (SAR≈30) was prepared by a similar method as described in Example 1, in which 3,5-DMP was used as the co-template. The final gel with molar composition of H₂O:SiO₂:Al₂O₃:2,6-DMP-OH:3,5-DMP-OH=25:1:0.033:0.25:0.2 was rotated in the oven at 155° C. for 5 days. Analysis of the as made product by powder XRD indicated that the product had a AEI structure, and the sample has rectangular parallelepiped morphology (SEM image as shown in FIG. 3).

Example 4: Preparation of H-AEI Zeolite Using a Mixture of 2,6-DMP-OH and TPA-OH as the SDAs

H-AEI (SAR≈30) was prepared by a similar method as described in Example 1, in which TPA-OH was used as the co-template. The final gel with molar composition of H₂O:SiO₂:Al₂O₃:2,6-DMP-OH:TPA-OH=25:1:0.033:0.25:0.2 was rotated in the oven at 155° C. for 5 days. Analysis of the as made product by powder XRD indicated that the product had a AEI structure, and the sample has the particle morphology as shown in FIG. 4.

Example 5: Preparation of Alkali-Free One-Pot Cu-AEI Zeolite Using a Mixture of 2,6-DMP-OH and Cu(TETA)²⁺ as the SDAs

One pot Cu-AEI was prepared by a similar method as described in Example 1, in which Cu(TETA)²⁺ was used as the co-template and copper source, CBV712 and CBV720 were used as both Si and Al sources. The final gel with molar composition of H₂O:SiO₂:Al₂O₃:2,6-DMP-OH:Cu(TETA)²⁺=25:1:0.038:0.45:0.025 was rotated in the oven at 155° C. for 5 days. Analysis of the as-made product by powder XRD indicated that the product had a AEI structure.

Example 6: SCR Testing on Copper Exchanged Zeolite Catalysts

Synthesis of Copper Exchanged AEI:

˜2.5-3% wt of copper exchanged into the calcined prepared by conventional route AEI (SAR≈20), and H-AEI zeolite (SAR≈30, example 1) using Cu(CH₃COO)₂.

Testing Conditions:

SV=90K, 500 ppm NH₃, 500 ppm NO, 4.6% H₂O, 14% O₂, 5% CO₂ in N₂. Ramp 5° C./min.

Procedures:

Catalyst was initially exposed to full gas mixture with NH₃ for 10 min at 150° C. NH₃ was switched on and the catalyst is stabilized for 30 min to saturate. Catalyst was then evaluated during a 5° C./min ramp from 150 to 500° C. Catalyst was evaluated at steady state at 500° C. then cooled and evaluated again at steady state at 250° C.

FIG. 5a shows NOx conversions on 3% Cu.AEI (SAR≈20) and Cu.H-AEI (SAR≈30, H-AEI from Example 1), with ˜2.5% wt of copper exchanged into the AEI zeolites.

FIG. 5b shows N₂O selectivity of reference 3% Cu.AEI (SAR≈20) and 2.5% Cu.H-AEI (SAR≈30, H-AEI from Example 1) of the present invention. High silica Cu.AEI (SAR≈30) of the present invention demonstrated similar fresh SCR activities as lower silica Cu.AEI (SAR≈20) even with slightly lower Cu loading, and it showed some advantages on the N₂O selectivity over the catalyst from the reference AEI (SAR≈20). Catalyst 2.5% Cu.H-AEI also showed excellent hydrothermal durability after aging at 900° C./5 h/4.5% H₂O.

FIG. 5c shows NO_(X) conversions on reference 3% Cu.AEI (SAR≈20) and one-pot Cu-AEI (Example 5).

FIG. 5d shows N₂O selectivity of reference 3% Cu.AEI (SAR≈20) and one-pot Cu-AEI (Example 5).

Alkali-free one-pot Cu-AEI of the present invention demonstrated similar fresh SCR activities as the reference Cu.AEI (SAR≈20), and it showed high advantages on the N₂O selectivity over the catalyst from the reference AEI (SAR≈20).

The above examples are set forth to aid in the understanding of the disclosure, and are not intended and should not be construed to limit in any way the disclosure set forth in the claims which follow hereafter. Although illustrated and herein described with reference to certain specific embodiments, the present disclosure is nevertheless not intended to be limited to the details shown, but various modifications may be made therein without departing from the spirit of the disclosure. 

What is claimed is:
 1. A method of synthesizing a zeolite comprising the steps of: a. preparing an admixture containing (i) at least one source of alumina, (ii) at least one source of silica, and (iii) at least one structure directing agent (SDA) in hydroxide form, wherein the admixture is essentially free of alkali metals, wherein the admixture has the following composition: Ratios SiO₂/OH 1-4 SiO₂/SDA(s) 1-4 H₂O/SiO₂ 10-40 alkali metal/SiO₂ 0 Al₂O₃/SiO₂ 0.02-0.05

and wherein the at least one structure directing agent (SDA) in hydroxide form is N,N-diethyl-2,6-dimethylpiperidinium; and b. heating the admixture under autogenous pressure at a temperature and with stirring or mixing for a sufficient time to crystalize hydrogen-form zeolite crystals having an AEI framework.
 2. The method of claim 1, wherein the admixture is essentially free of metal ions, other than aluminum.
 3. The method of claim 1, wherein the molar ratio of SDA to silica is greater than 0.4:1.
 4. The method of claim 1, wherein the yield on silica is at least about 50%.
 5. The method of claim 1, wherein the sources of silica and alumina are faujasite zeolites.
 6. The method of claim 1, wherein the admixture has the following composition: Ratios SiO₂/OH 1.5-2.5 SiO₂/SDA(s) 1.5-2.5 H₂O/SiO₂ 15-30 alkali metal/SiO₂ 0 Al₂O₃/SiO₂  0.025-0.04. 


7. The method of claim 1, further comprising a second SDA.
 8. The method of claim 7, wherein the second SDA is selected from 3,5-DMP, trimethyl cyclohexylammonium (TMCHA), tetraethylammonium (TEA), Dimethyldipropylammonium (DMDPA), tetrapropylammonium (TPA), tetraethylphosphonium (TEP).
 9. The method of claim 7, wherein the second SDA is N,N-Dimethyl-3,5-dimethylpiperidinium. 